CN101892066A - Production technology for cracking butyl octanol residual liquid into C4 and C8 by means of alkaline liquid cracking agent - Google Patents
Production technology for cracking butyl octanol residual liquid into C4 and C8 by means of alkaline liquid cracking agent Download PDFInfo
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- CN101892066A CN101892066A CN2010101014770A CN201010101477A CN101892066A CN 101892066 A CN101892066 A CN 101892066A CN 2010101014770 A CN2010101014770 A CN 2010101014770A CN 201010101477 A CN201010101477 A CN 201010101477A CN 101892066 A CN101892066 A CN 101892066A
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- Prior art keywords
- alkaline liquid
- cracking agent
- carbon
- cracking
- liquid cracking
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- 238000005336 cracking Methods 0.000 title claims abstract description 37
- 239000007788 liquid Substances 0.000 title claims abstract description 29
- 238000004519 manufacturing process Methods 0.000 title claims abstract description 13
- 238000005516 engineering process Methods 0.000 title abstract description 10
- XMVBHZBLHNOQON-UHFFFAOYSA-N 2-butyl-1-octanol Chemical compound CCCCCCC(CO)CCCC XMVBHZBLHNOQON-UHFFFAOYSA-N 0.000 title abstract 3
- 239000003795 chemical substances by application Substances 0.000 claims abstract description 25
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical compound [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 claims abstract description 18
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 claims abstract description 18
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims abstract description 12
- JKWMSGQKBLHBQQ-UHFFFAOYSA-N diboron trioxide Chemical compound O=BOB=O JKWMSGQKBLHBQQ-UHFFFAOYSA-N 0.000 claims abstract description 12
- 238000000034 method Methods 0.000 claims abstract description 10
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 9
- 229910001868 water Inorganic materials 0.000 claims abstract description 9
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 claims abstract description 7
- 239000012286 potassium permanganate Substances 0.000 claims abstract description 6
- KBPLFHHGFOOTCA-UHFFFAOYSA-N 1-Octanol Chemical compound CCCCCCCCO KBPLFHHGFOOTCA-UHFFFAOYSA-N 0.000 claims description 58
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 24
- 229910052799 carbon Inorganic materials 0.000 claims description 24
- 238000000605 extraction Methods 0.000 claims description 18
- 241000282326 Felis catus Species 0.000 claims description 15
- 239000000470 constituent Substances 0.000 claims description 15
- 229910002651 NO3 Inorganic materials 0.000 claims description 5
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 claims description 5
- QVQLCTNNEUAWMS-UHFFFAOYSA-N barium oxide Chemical compound [Ba]=O QVQLCTNNEUAWMS-UHFFFAOYSA-N 0.000 claims description 5
- 229910001864 baryta Inorganic materials 0.000 claims description 5
- 238000000926 separation method Methods 0.000 claims description 3
- LYCAIKOWRPUZTN-NMQOAUCRSA-N 1,2-dideuteriooxyethane Chemical compound [2H]OCCO[2H] LYCAIKOWRPUZTN-NMQOAUCRSA-N 0.000 claims description 2
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 abstract description 12
- 238000005194 fractionation Methods 0.000 abstract description 3
- 238000000998 batch distillation Methods 0.000 abstract description 2
- IWOUKMZUPDVPGQ-UHFFFAOYSA-N barium nitrate Chemical compound [Ba+2].[O-][N+]([O-])=O.[O-][N+]([O-])=O IWOUKMZUPDVPGQ-UHFFFAOYSA-N 0.000 abstract 2
- 238000001944 continuous distillation Methods 0.000 abstract 1
- 238000005086 pumping Methods 0.000 abstract 1
- 239000004615 ingredient Substances 0.000 description 4
- 239000010865 sewage Substances 0.000 description 3
- AVERNHDYEFYHIV-UHFFFAOYSA-N dodecan-5-ol Chemical group CCCCCCCC(O)CCCC AVERNHDYEFYHIV-UHFFFAOYSA-N 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000006378 damage Effects 0.000 description 1
- 230000007812 deficiency Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000003912 environmental pollution Methods 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 238000006116 polymerization reaction Methods 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 238000010992 reflux Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
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Abstract
The invention relates to production technology for cracking butyl octanol residual liquid into C4 and C8 by means of an alkaline liquid cracking agent. The technology is characterized by comprising the following steps of: preparing the alkaline liquid cracking agent, wherein the alkaline liquid cracking agent consists of sodium hydroxide, potassium hydroxide, water, isopropanol, ethylene glycol, potassium permanganate, ethanol, barium nitrate and diboron trioxide; preheating the alkaline liquid cracking agent and the butyl octanol residual liquid through a preheater and adding into a distilling still, wherein the tower bottom temperature of the distilling still is between 200 and 280 DEG C, the tower top temperature is between 130 and 190 DEG C, and the tower top pressure is between 0.08 and 0.1MPa below zero; and extracting the C4 and C8 generated by cracking from the tower top of the distilling still, pumping the C4 and C8 into a fractionating column at the downstream for fractionation, and extracting a small amount of uncracked heavy components from a tower bottom pump. The production technology has the advantages of high production capacity, high cracking selectivity, high content of the cracked useful components, low cost, simple process, and batch distillation or continuous distillation.
Description
Technical field
The present invention relates under a kind of alkaline liquid cracking agent fourth octanol raffinate is cracked into the production technique of carbon four and carbon eight, belong to petrochemical industry.
Background technology
At present in the world, petrochemical enterprise is in the production process of fourth octanol, the fourth octanol raffinate that butyl octanol unit is discharged contains a large amount of C12～C16 components owing to the polymerization generation, but the domestic existing device can not rationally utilize this resource, can only be to fall as sewage disposal, not only waste a large amount of resources, also environment has been caused destruction.If this part fourth octanol raffinate is recovered utilization, not only can reduce environmental pollution, can also cracking produce value very high C4 and C8 component, have very big social benefit and economic benefit.
Summary of the invention
According to above deficiency of the prior art, the technical problem to be solved in the present invention is: provide a kind of fourth octanol raffinate is cracked into the production technique of carbon four and carbon eight, this technology is simple, and cost is low, pollutes few.
The technical solution adopted for the present invention to solve the technical problems is: the production technique that under a kind of alkaline liquid cracking agent fourth octanol raffinate is cracked into carbon four and carbon eight, it is characterized in that disposing the alkaline liquid cracking agent, the quality group of alkaline liquid cracking agent becomes: sodium hydroxide 5%～15%, potassium hydroxide 10%～30%, water 10%～30%, Virahol 5%～15%, ethylene glycol 2%～10%, potassium permanganate 2%～10%, ethanol 5%～10%, nitrate of baryta 1%～5%, boron trioxide 1%～5% joins this alkaline liquid cracking agent and fourth octanol raffinate in the still kettle after the preheater preheating together, and control preheater temperature is 150 ℃～200 ℃, still kettle tower still temperature is 200 ℃～280 ℃, tower top temperature is 130 ℃～190 ℃, tower top pressure is-and 0.08Mpa～-0.1Mpa, carbon four that fourth octanol raffinate generates after cracking and carbon eight useful components are from the cat head extraction of still kettle, fractionate out carbon four and carbon eight components through separation column, a small amount of uncracked heavy constituent by tower at the bottom of extraction.
Carbon four and carbon eight blending ingredients carry out the fractionation of carbon four and carbon eight according to the public technology mode.
The add-on of described alkaline liquid cracking agent is 0.2%～1.0% of a fourth octanol raffinate inlet amount quality.
But but this also periodical operation of technology multitower operate continuously.
The main quality group of fourth octanol raffinate of the present invention becomes: C4＜1%, C8＜1%, heavy constituent (C12 and C16) 98%～99%.
Cat head extraction useful component is the 70%-80% of fourth octanol raffinate quality after cracking, and wherein C4 is 30%～45% of a cat head extraction constituent mass, and C8 is 45%～55% of a cat head extraction constituent mass.
The beneficial effect that the present invention had is:
The present invention is a kind of production technique that fourth octanol raffinate is cracked into carbon four and carbon eight under the alkaline liquid cracking agent, and throughput is big, and the cracking selectivity is good, the useful component content height that cracking goes out, and cost is low, and technology is simple, but but also continuous still battery of batch distillation.By the cracking to fourth octanol raffinate, make resource obtain reasonable use more simultaneously, the resource as sewage discharge has obtained utilizing again originally, makes that ample resources obtains recycling; Reduce the discharging of large amount of sewage, made environment obtain effective assurance, had very big social benefit and economic worth.
Description of drawings
Fig. 1 is a process flow sheet of the present invention.
Embodiment
The technological process of production of the present invention is: fourth octanol raffinate and alkaline liquid cracking agent from butyl octanol unit converge after after the preheater preheating, be sent in the still kettle, the alkaline liquid cracking agent is by 0.2%～1.0% adding of the charging quality of fourth octanol raffinate, this cover water distilling apparatus comprises conventional feed preheater, distillation tower, tower still reboiler, the cat head water cooler, vacuum pump, return tank and impeller pump etc. are partly formed, heat by tower still reboiler, make the preheater temperature be controlled at 150 ℃～200 ℃, tower still temperature is controlled at 200 ℃～280 ℃, tower top temperature is controlled at 130 ℃～190 ℃ by cat head water cooler and quantity of reflux, tower top pressure vacuum available pump is controlled at-0.08Mpa～-0.1Mpa, by trim the top of column pump extraction useful component C4 and C8 through condenser to return tank, be pumped in the separation column in downstream by public technology through trim the top of column then and carry out the fractionation of C4 and C8, a small amount of uncracked heavy constituent are by the column bottoms pump extraction.
Embodiment 1:
The quality group of alkaline liquid cracking agent becomes: sodium hydroxide 15%, potassium hydroxide 30%, water 20%, Virahol 12%, ethylene glycol 7%, potassium permanganate 6%, ethanol 8%, nitrate of baryta 1%, boron trioxide 1%.
Fourth octanol raffinate is mainly formed: C4 is 0.7%, and C8 is 0.8%, and heavy constituent (C12 and C16) are 98.5%.
When the inlet amount of fourth octanol raffinate accounted for still kettle volume 50%, the add-on of alkaline liquid cracking agent was 0.5% of a raw materials quality, 150 ℃ of preheater temperature, and tower still temperature is 220 ℃, and tower top temperature is 150 ℃, and tower top pressure is-0.08Mpa.80% of cat head extraction ingredients constitute fourth octanol raffinate quality, the produced quantity of C4 accounts for 42% of cat head extraction constituent mass, and the produced quantity of C8 accounts for 51% of cat head extraction constituent mass.
Embodiment 2:
The quality group of alkaline liquid cracking agent becomes: sodium hydroxide 5%, potassium hydroxide 10%, water 30%, Virahol 15%, ethylene glycol 10%, potassium permanganate 10%, ethanol 10%, nitrate of baryta 5%, boron trioxide 5%.
Fourth octanol raffinate is mainly formed: C4 is 0.5%, and C8 is 0.9%, and heavy constituent (C12 and C16) are 98.6%.
When the inlet amount of fourth octanol raffinate accounted for still kettle volume 60%, the add-on of alkaline liquid cracking agent was 0.6% of a material quantity, and the preheater temperature is 180 ℃, and tower still temperature is 240 ℃, and tower top temperature is 170 ℃, and tower top pressure is-0.09Mpa.76% of cat head extraction ingredients constitute fourth octanol raffinate quality, the produced quantity of C4 accounts for 41% of cat head extraction constituent mass, and the produced quantity of C8 accounts for 53% of cat head extraction constituent mass.
Embodiment 3:
The quality group of alkaline liquid cracking agent becomes: sodium hydroxide 10%, potassium hydroxide 25%, water 25%, Virahol 10%, ethylene glycol 8%, potassium permanganate 8%, ethanol 7%, nitrate of baryta 4%, boron trioxide 3%.
Fourth octanol raffinate is mainly formed: C4 is 0.4%, and C8 is 0.8%, and heavy constituent (C12 and C16) are 98.8%.
When the inlet amount of fourth octanol raffinate accounted for still kettle volume 70%, the add-on of alkaline liquid cracking agent was 0.7% of a material quantity, and the preheater temperature is 200 ℃, and tower still temperature is 260 ℃, and tower top temperature is 185 ℃, and tower top pressure is-0.1Mpa.74% of cat head extraction ingredients constitute fourth octanol raffinate quality, the produced quantity of C4 accounts for 39% of cat head extraction constituent mass, 54% of the produced quantity cat head extraction constituent mass of C8.
Claims (2)
1. under the alkaline liquid cracking agent fourth octanol raffinate is cracked into the production technique of carbon four and carbon eight, it is characterized in that preparing the alkaline liquid cracking agent, the quality group of alkaline liquid cracking agent becomes: sodium hydroxide 5%～15%, potassium hydroxide 10%～30%, water 10%～30%, Virahol 5%～15%, ethylene glycol 2%～10%, potassium permanganate 2%～10%, ethanol 5%～10%, nitrate of baryta 1%～5%, boron trioxide 1%～5% joins this alkaline liquid cracking agent and fourth octanol raffinate in the still kettle after the preheater preheating together, and control preheater temperature is 150 ℃～200 ℃, still kettle tower still temperature is 200 ℃～280 ℃, tower top temperature is 130 ℃～190 ℃, tower top pressure is-and 0.08Mpa～-0.1Mpa, carbon four that fourth octanol raffinate generates after cracking and carbon eight useful components are from the cat head extraction of still kettle, fractionate out carbon four and carbon eight components through separation column again, a small amount of uncracked heavy constituent by tower at the bottom of extraction.
2. according to the described production technique of claim 1, the add-on that it is characterized in that described alkaline liquid cracking agent is 0.2%～1.0% of a fourth octanol raffinate inlet amount quality.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010101477 CN101892066B (en) | 2010-01-27 | 2010-01-27 | Production technology for cracking butyl octanol residual liquid into C4 and C8 by means of alkaline liquid cracking agent |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN 201010101477 CN101892066B (en) | 2010-01-27 | 2010-01-27 | Production technology for cracking butyl octanol residual liquid into C4 and C8 by means of alkaline liquid cracking agent |
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| Publication Number | Publication Date |
|---|---|
| CN101892066A true CN101892066A (en) | 2010-11-24 |
| CN101892066B CN101892066B (en) | 2013-01-23 |
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| CN 201010101477 Expired - Fee Related CN101892066B (en) | 2010-01-27 | 2010-01-27 | Production technology for cracking butyl octanol residual liquid into C4 and C8 by means of alkaline liquid cracking agent |
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Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104447194A (en) * | 2014-11-11 | 2015-03-25 | 中国海洋石油总公司 | Method for processing butyl-octyl alcohol residual liquid |
| CN113262704A (en) * | 2021-05-27 | 2021-08-17 | 聊城鲁西多元醇新材料科技有限公司 | Cracking catalyst preparation system and method and application thereof |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101172725A (en) * | 2006-10-31 | 2008-05-07 | 中国石油化工股份有限公司 | Method for processing waste alkali liquid in butyl octanol production |
| CN101423455A (en) * | 2008-12-03 | 2009-05-06 | 沈晓东 | Butanol-octanol waste oil and 2-PH waste oil resource treatment method |
-
2010
- 2010-01-27 CN CN 201010101477 patent/CN101892066B/en not_active Expired - Fee Related
Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN101172725A (en) * | 2006-10-31 | 2008-05-07 | 中国石油化工股份有限公司 | Method for processing waste alkali liquid in butyl octanol production |
| CN101423455A (en) * | 2008-12-03 | 2009-05-06 | 沈晓东 | Butanol-octanol waste oil and 2-PH waste oil resource treatment method |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN104447194A (en) * | 2014-11-11 | 2015-03-25 | 中国海洋石油总公司 | Method for processing butyl-octyl alcohol residual liquid |
| CN113262704A (en) * | 2021-05-27 | 2021-08-17 | 聊城鲁西多元醇新材料科技有限公司 | Cracking catalyst preparation system and method and application thereof |
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| CN101892066B (en) | 2013-01-23 |
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Effective date of registration: 20210806 Address after: 257500 North of Meichen South Road, Kenli Development Zone, Dongying City, Shandong Province Patentee after: Shandong Ruilier Petroleum Equipment Co.,Ltd. Address before: 255400 9-1-501, zone 2, Erhua living area, Linzi District, Zibo City, Shandong Province Patentee before: Yang Baoli |
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Granted publication date: 20130123 |